AT525775A1 - Arrangement, refinery and process for the production of hydrocarbons - Google Patents

Abstract

The invention relates to an arrangement, a refinery and a process for the production of hydrocarbons, the arrangement comprising a cracking device (1) and a feed arrangement (2), the feed arrangement (2) of the cracking device (1) containing a feed stream (5) which contains hydrocarbons and supplies steam (6), the cracking device (1) being set up for steam cracking the hydrocarbons, the arrangement having a hydrogen production device (3), in particular an electrolyzer for water electrolysis and/or a reforming device, preferably a steam reforming device (12) or a methane pyrolysis device, wherein the hydrogen production device (3) is set up for the production of, in particular so-called green, hydrogen (7), wherein the feed arrangement (2) at least a part of the hydrogen production device (3) produced hydrogen (7), in particular so-called green hydrogen (7) to the cracking device (1), the cracking device (1) producing hydrocarbons, and the hydrocarbons produced being composed at least partially of the hydrogen (7), in particular the so-called green hydrogen, produced by the hydrogen production device (3).

Description

Arrangement, refinery and process for the production of hydrocarbons

The invention relates to an arrangement, a refinery and a method according to

Preambles of the independent claims.

Different arrangements for the production of hydrocarbons are known from the prior art. For example, arrangements are known in which only hydrocarbons and steam are fed to a steam cracker. A disadvantage of these conventional methods, however, is that on the one hand only conventional hydrocarbons can be produced as a result. On the other hand, such conventional steam crackers emit a lot of carbon dioxide, so they significantly to

contribute to global CO2 production.

The object of the invention is to overcome the disadvantages of the prior art. In particular, the object of the invention is to create an arrangement, a refinery and a method for increasing the efficiency and environmental friendliness of cracking devices, in particular steam crackers. Among other things, it is an object of the invention to provide an arrangement, a refinery and a method with which the combustion emissions, such as in particular the carbon dioxide, nitrogen oxide and / or dust emissions, the cracking device lowered and the

Efficiency of the cracking device can be increased.

The object of the invention is in particular due to the features of

independent patent claims solved.

The invention relates in particular to an arrangement for the production of hydrocarbons comprising a cracking device, in particular one

steam cracker, and at least one feed assembly.

The feed assembly preferably feeds the cracker a feed stream which

Contains hydrocarbons and vapor too.

The cracker is preferred for steam cracking the hydrocarbons

furnished.

The cracker is preferred for converting longer chain ones

Hydrocarbons furnished with vapor to form short-chain hydrocarbons.

Provision is preferably made for the arrangement to be a hydrogen production device

includes.

It is preferably provided that the hydrogen production device as an electrolyzer for water electrolysis and / or as a reforming device, in particular as

Steam reforming device or as a methane pyrolysis device is formed.

It is preferably provided that the hydrogen production device for the production of

in particular so-called green, hydrogen is set up.

In particular, the emissions per tonne of ethene produced and/or HVC produced in the cracking device can be lower than in the case of a cracking device without the supply of hydrogen as a result of the supply of, in particular so-called green, hydrogen. Within the scope of the present invention, emissions can include carbon dioxide, nitrogen oxides and/or

dust are understood.

Provision is preferably made for the supply arrangement to supply at least part of the hydrogen produced by the hydrogen production device, in particular

so-called green hydrogen feeding the cracker.

It is preferably provided that the cracking device produces hydrocarbons.

It is preferably provided that the hydrocarbons produced are at least partially made up of, in particular, the hydrocarbons produced by the hydrogen production device

the so-called green hydrogen.

It is preferably provided that the hydrocarbons produced at least partially the produced by the hydrogen production device, in particular the

so-called green, have hydrogen.

In particular, the invention relates to an arrangement for the production of, in particular green, hydrocarbons which are at least partially made from green hydrogen

consist.

In the context of the present invention, a cracking device, in particular a steam cracker, can be understood to mean a conventional cracking device, in particular a conventional steam cracker. So-called steam cracking and/or steam cracking can be a conventional petrochemical process. In steam cracking, longer-chain hydrocarbons, in particular naphtha, propane, butane, ethane, gas oil and/or hydrowax, are optionally broken down by thermal cracking in the presence of steam

converted to short-chain hydrocarbons.

In the context of the present invention, green hydrogen can be understood to mean hydrogen that is generated through the use of renewable energies, such as in particular solar energy, bioenergy, hydropower and/or wind energy

becomes.

In the context of the present invention, green hydrogen can also be understood to mean that hydrogen whose addition to use in the cracking device leads to emissions, in particular of carbon dioxide, so-called CO », nitrogen oxides, so-called NOx, and / or dust, and the like , per tonne of high-value chemicals produced, so-called HVC, and/or ethene are falling. This may mean that by feeding green hydrogen into the cracking device, the emissions produced per ton of HVC and/or ethene are reduced compared to conventional production processes

can.

So-called green hydrogen can, if necessary, be obtained in a CO »neutral manner, so that in particular the overall efficiency of the arrangement, in particular the

Cracking device that can be increased.

As a rule, it may be customary in conventional refineries for more hydrogen to be produced than is required. This ensures, if necessary, that all conventional hydrogen consumers of a refinery, such as in particular

Hydrogenation plants, can be adequately supplied.

In a conventional refinery, the overproduction of hydrogen is optionally flared off and/or thermally utilized. In particular, this hydrogen, especially if too much is produced, can be added to the use of the cracking device, which may reduce the emissions per tonne of ethene or

HVC can be significantly reduced.

Therefore, in the context of the invention, so-called green hydrogen can also be understood to mean this hydrogen. In other words, within the scope of this invention, hydrogen may be considered green, regardless of production, as long as the hydrogen is sufficiently emission-neutral

can be obtained.

In the context of the present invention, under, in particular the so-called

green, hydrogen molecular hydrogen, namely H2, are understood.

In the context of the present invention, green and/or sustainably produced hydrocarbons can be understood to mean hydrocarbons which

are formed at least partially from so-called green hydrogen and/or

which consist at least partially of so-called green hydrogen and/or

which at least partially comprise so-called green hydrogen.

Optionally, conventional hydrogen, namely H 2 , can also be supplied at least in part to the cracking device. In the context of the present invention, conventional hydrogen can be understood as meaning hydrogen,

which is not generated using renewable energy sources.

In particular, conventional hydrogen can be understood in the context of the present invention as hydrogen, the addition of which to use in the cracking device does not lead to a reduction in emissions, in particular of CO, NOx and/or dust and the like, per t of HVC or ethene produced. In other words, so-called conventional hydrogen can be understood to mean that which is not obtained in a CO,2-neutral manner, so that the overall efficiency of the arrangement, in particular the cracking device, may be reduced

cannot be increased.

In other words, it can be provided that in the case of the hydrocarbons produced, the so-called green hydrogen with the carbon atoms

connected is.

If necessary, it is provided that the molecular, in particular so-called green, hydrogen with the input stream, in particular with the hydrocarbons, which

fed to the cracker is mixed. If necessary, it is provided that the molecular, in particular so-called green,

Hydrogen mixed with the steam fed to the cracker

becomes.

In the context of the present invention, the feed stream optionally includes hydrocarbons, which are fed to the cracking device, in particular to the steam cracker. In particular, the hydrocarbons fed to the cracking device, in particular the steam cracker, can be contained exclusively in the feed stream.

In the context of the present invention, a feed stream can be understood to mean a mass flow which the arrangement, in particular the cracking device,

preferably the steam cracker.

In the context of the present invention, feed stream can be understood to mean a mass flow which is fed into the arrangement, in particular into the cracking device,

preferably in the steam cracker.

In the context of the present invention, a mass flow can be understood under output flow, which from the arrangement, in particular from the

Cracking device, preferably from the steam cracker, is discharged.

In the context of the present invention, a mass flow can be understood under output flow, which from the arrangement, in particular from the

Cracking device, preferably from the steam cracker exits.

If necessary, the reactions that also take place in conventional cracking devices essentially take place in the cracking device. This makes it possible, if necessary, to combine the hydrogen supplied with that of the cracking device

to chemically combine supplied hydrocarbons.

The feed assembly optionally carries the output stream of the cracker

as a product of the arrangement.

The feed arrangement optionally carries at least part of the output stream

the cracker to a separator.

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The feed arrangement optionally feeds the hydrocarbons separated off in the separation device, in particular those from the output stream of the cracking device

separated hydrocarbons, as a product from the arrangement.

If necessary, it is provided that the arrangement electricity from a renewable energy source, in particular from solar energy, bioenergy, hydropower and / or

wind energy.

If necessary, it is provided that the hydrogen production device uses electricity, preferably exclusively, from a renewable energy source, in particular from

solar energy, bioenergy, hydroelectric power and/or wind energy.

If necessary, it is provided that the arrangement is a renewable energy source, in particular a solar energy utilization device, a bioenergy utilization device, a hydroelectric power utilization device and/or a

Wind energy harvesting device includes.

If necessary, it is provided that the hydrogen production device of the arrangement,

preferably exclusively, powered by the renewable energy source.

Optionally, it is provided that the hydrogen production device, in particular

so-called green, produces hydrogen.

If necessary, the reactions that also take place in conventional hydrogen production devices essentially take place in the hydrogen production device. This makes it possible, if necessary, to break down water into hydrogen and oxygen with the help of electricity. Since the electricity may come from a renewable energy source, it is possible to use the

Produce hydrogen production device so-called green hydrogen. Optionally, it is provided that the feeding arrangement, in particular one

Combustion chamber, the cracking device a fuel, in particular a heating gas,

preferably methane.

If necessary, it is provided that the supply arrangement for burning the fuel of the cracking device, in particular the combustion chamber of the cracking device, supplies oxygen and/or air.

If necessary, it is provided that the oxygen supplied to the combustion chamber

in particular exclusively, is produced by the hydrogen production device.

If necessary, it is provided that the oxygen supplied to the combustion chamber, in particular exclusively, is that produced during the electrolysis of water

is oxygen.

Optionally, it is provided that the oxygen produced by the hydrogen production device, in particular before entering the cracking device, with the

Fuel and / or optionally supplied air is mixed.

If necessary, it is provided that the oxygen produced during the electrolysis of water, in particular before it enters the cracking device, with the fuel

and/or the optionally supplied air is mixed.

If necessary, it is provided that the arrangement has at least one

Separator includes.

If appropriate, it is provided that a separation device separates the molecular, in particular green, hydrogen contained in the output stream of the cracking device, in particular completely, from that contained in the output stream of the cracking device

hydrocarbons separated. If necessary, it is provided that the feed arrangement feeds the molecular hydrogen, in particular green hydrogen,

especially complete, feeding the cracker.

Optionally, it is provided that an exit of the molecular hydrogen from the

Arrangement is essentially prevented or reduced.

Optionally, it is provided that an exit of the molecular hydrogen from the

Cracking device is substantially prevented or reduced.

If necessary, it is provided that the separation device separates the molecular, in particular green, hydrogen from the output stream of the arrangement,

in particular the cracker, separates.

If necessary, it is provided that the feed arrangement separates the molecular, in particular green, hydrogen of the arrangement, in particular the

Cracking device and / or the hydrogenation plant supplied.

By separating and resupplying the molecular hydrogen in the arrangement is optionally an exit of the molecular hydrogen from the

Arrangement, in particular the cracker, prevented or reduced.

Through the arrangement and/or the process, in particular through the supply of, in particular molecular, preferably the so-called green hydrogen, it is possible to reduce the difference in enthalpy between the feed stream on entry into the cracking device, in particular on entry into the cracking device of the cracker, and the output stream on exit from the cracker, particularly on exit from the splitter of the cracker. This makes it possible, if necessary, to use fuel, in particular

fuel gas to reduce.

Furthermore, the cracking device is optionally heated with a heating device which is operated by the or another renewable energy source. In particular, the heating device can be an electrical resistance heater, an electrically heated thermodynamic radiation source and/or an infrared radiator, which is operated in particular by a renewable energy source. This makes it possible, if necessary, to achieve the same heating output with fewer emissions than with

to produce conventional crackers. In other words can

if necessary, the required heating output with fewer emissions than with

conventional crackers are generated.

In the context of the present invention, fuel can be understood to mean a heating gas, in particular a combustible gas such as methane. The synergistic use of the oxygen produced by the hydrogen production facility may reduce the formation of nitrogen oxides in the cracking facility. In other words, the amount of air needed, which also includes nitrogen, can be increased through the synergistic use of the

produced oxygen are reduced, thereby reducing emissions.

Optionally, it is provided that the arrangement is a reforming device, in particular a steam reforming device or a

Methane pyrolysis device.

If necessary, it is provided that the feed arrangement covers at least a part of the

Output stream of the cracker of the reformer feeds.

If necessary, it is provided that the feed arrangement covers at least a part of the

methane contained in the output stream feeds the reforming device.

Optionally, it is provided that the output stream of the cracking device, in particular the hydrocarbons contained in the output stream, at least partially from the produced by the hydrogen production device, in particular

the so-called green, hydrogen.

If necessary, it is provided that the methane contained in the output stream of the cracking device is at least partially made up of the methane produced by the hydrogen production device, in particular the so-called green

hydrogen exists.

Optionally, it is provided that the reforming device for the production of

Hydrogen from methane is set up.

If necessary, it is provided that the reforming device molecular,

in particular so-called green, produces hydrogen.

The reforming device is optionally set up to produce molecular hydrogen, in particular so-called green hydrogen, from the supplied hydrocarbons, which in particular contain so-called green hydrogen

produce hydrogen.

The feeding arrangement may be that produced by the reforming device

Feed hydrogen to the cracking device, in particular to the steam cracker.

The feeding arrangement may be that produced by the reforming device

Supply hydrogen to the hydrogenation plant.

In the context of the present invention, a portion of the effluent from the cracker can be understood to mean at least a portion of the effluent from the cracker and/or at least a portion of the effluent from the separator downstream of the cracker. In other words, it is preferably provided that that part of the output stream from the cracking device which is fed to the reforming device contains, in particular, essentially exclusively hydrocarbons and/or is essentially free of them

molecular hydrogen is.

If necessary, it is provided that the arrangement includes a hydrogenation plant. If necessary, it is provided that the feed arrangement feeds at least part of the output stream of the cracking device, which contains in particular hydrocarbons, to the hydrogenation plant.

If necessary, it is provided that the feed arrangement covers at least a part of the

Output stream of the separator, which in particular hydrocarbons

contains, the hydrogenation system feeds.

If appropriate, it is provided that the output stream of the cracking device optionally consists at least partially of the hydrogen produced by the hydrogen production device, in particular the so-called green hydrogen. If necessary, it is provided that the hydrocarbons in the output stream of the cracking device, if necessary at least partly from the hydrocarbons produced by the hydrogen production device, in particular the so-called green,

hydrogen exist.

If necessary, it is provided that the feed arrangement supplies at least a part of the hydrogen production device and/or the reforming device

hydrogen produced feeds the hydrogenation plant.

If necessary, it is provided that the hydrogenation plant for the hydrogenation of

Hydrocarbons is set up.

Optionally, it is provided that the hydrogenation plant produces hydrocarbons, the hydrocarbons produced at least partially from the produced by the hydrogen production device, in particular the so-called

green, hydrogen exist.

If necessary, it is provided that the hydrocarbons produced by the hydrogenation plant consist of more, in particular green, hydrogen than that of the

Hydrocarbons supplied to the hydrogenation plant.

In the context of the present invention, hydrogenation can be understood as meaning the addition of hydrogen to other chemical elements or compounds. In particular, within the scope of the present invention, hydrogenation means the so-called selective hydrogenation of the undesired carbon

understand carbon bonds.

The hydrogenation plant is optionally set up from the supplied

Hydrocarbon, which contains in particular the so-called green hydrogen,

in particular hydrogenated hydrocarbons, which in particular so-called green

contain hydrogen to produce.

The feed arrangement optionally feeds the output stream of the hydrogenation plant

as a product of the arrangement.

The feed arrangement optionally carries at least part of the output stream

the hydrogenation plant to a separation device.

The at least one separation device can be set up to separate the molecular hydrogen from the other molecules contained in the output stream, in particular in the output stream of the hydrogenation plant, in particular hydrocarbons

Substantially completely separate.

The feeder leads the separated molecular hydrogen

Cracking device and / or the hydrogenation plant as a so-called recycle stream.

If necessary, the feed arrangement feeds the hydrocarbons separated off in the separation device, in particular those from the output stream of the hydrogenation plant

separated hydrocarbons, as a product from the arrangement.

In the context of the present invention, part of the output stream of the cracker can be understood to mean at least part of the output stream from the cracker and/or at least part of the output stream of the separator downstream of the cracker. In other words, it is preferably provided that that part of the output stream of the cracking device which is fed to the hydrogenation plant for the hydrogenation of hydrocarbons which contain more than 3 carbon atoms contains, in particular, essentially exclusively hydrocarbons and/or is essentially free of

molecular hydrogen is.

If necessary, it is provided that the arrangement comprises a metathesis system.

Optionally, it is provided that the feed arrangement supplies at least part of the output stream of the cracking device, which in particular contains hydrocarbons

contains, which feeds the metathesis system.

If necessary, it is provided that the output stream, in particular the hydrocarbons contained in the output stream, of the cracking device is at least partially made up of that produced by the hydrogen production device, in particular

the so-called green, hydrogen.

Optionally, it is envisaged that the metathesis unit for the conversion of hydrocarbons with four carbon atoms and ethene to hydrocarbons with

three hydrocarbon atoms is set up.

Optionally, it is provided that the metathesis plant for the conversion of 2-

butene and ethene to propene.

Optionally, it is provided that the metathesis plant produces hydrocarbons with three carbon atoms, the hydrocarbons produced with three carbon atoms being at least partially composed of the, in particular the so-called green,

hydrogen exist.

If appropriate, it is provided that the metathesis plant produces propene, the propene produced being at least partially composed of the, in particular the so-called green,

hydrogen exists.

In the context of the present invention, part of the output stream of the cracker can be understood to mean at least part of the output stream from the cracker and/or at least part of the output stream of the separator downstream of the cracker. In other words, it is preferably provided that the part of the output stream of the cracking device

which is fed to the metathesis system in particular essentially

contains only hydrocarbons and/or is essentially free of

molecular hydrogen is.

The feed arrangement optionally carries the output stream of the metathesis system

as a product of the arrangement.

The feed arrangement optionally carries at least part of the output stream

the metathesis system to a separation device.

If necessary, the feed arrangement feeds the hydrocarbons separated off in the separation device, in particular those from the output stream of the metathesis plant

separated hydrocarbons, as a product from the arrangement.

If necessary, it is provided that the feed arrangement of the cracking device supplies molecular, in particular so-called green, hydrogen in the range of 0.05 parts by weight, in particular 0.05% by weight, up to and including 5 parts by weight, in particular 5% by weight, in particular 0.5 parts by weight. In particular 0.5 wt.% Up to and including 1.5 parts by weight, in particular 1.5 wt.% Based on the

feed stream of the cracker feeds.

If necessary, it is provided that the feed arrangement of the cracking device supplies molecular, in particular so-called green, hydrogen in the range of 0.05 parts by weight, in particular 0.05% by weight, up to and including 5 parts by weight, in particular 5% by weight, in particular 0.5 parts by weight. In particular 0.5 wt.% Up to and including 1.5 parts by weight, in particular 1.5 wt.% Based on the

Hydrocarbons in the feed stream to the cracker.

If necessary, it is provided that the feed arrangement of the cracking device supplies molecular, in particular so-called green, hydrogen in the range of 0.05 parts by weight, in particular 0.05% by weight, up to and including 5 parts by weight, in particular 5% by weight, in particular 0.5 parts by weight. In particular 0.5 wt.% Up to and including 1.5 parts by weight, in particular 1.5 wt.% Based on the

so-called dry input current.

If necessary, it is provided that the feed arrangement of the hydrogenation plant molecular, in particular at least partially so-called green, hydrogen, in the range of more than 0.5 wt.%, In particular 0.5 mass fractions, based on the

Hydrocarbons in the feed stream to the hydrogenation plant.

In the context of the present invention, dry feed stream can be understood to mean the feed stream to the cracker which is essentially free

of water, in particular free of water vapor.

In the context of the present invention, the mass fractions can be understood to mean the mass fraction. In other words, the mass of a mixture component under consideration can be related to the sum of the masses of all mixture components, so that the mass fraction may be the relative proportion of the mass of a mixture component under consideration in the

indicates the total mass of the mixture.

Optionally, it is provided that the cracking device has at least one

Splitting device, a so-called gap coil includes.

If necessary, it is provided that the feed arrangement of the splitting device

Hydrocarbons, hydrogen and / or water feeds.

The mass flow in the splitting device, in particular in the splitting tube, has the so-called coin inlet temperature, abbreviated to CIT, at the inlet and the so-called coil outlet temperature, abbreviated to COT, at the outlet. The CIT can be approximately 600°C up to and including 650°C. The COT can be approx. 750°C up to and including 900°C

be. If necessary, it is provided that the temperature of the splitting device,

in particular the cracking tube, supplied hydrocarbon, the hydrogen

and/or the water is in the range of about 600°C to 650°C.

If necessary, the temperature of the supplied hydrocarbon, the hydrogen and/or the water in the inlet area of the cleavage device, in particular in the inlet area of the cracking tube of the cleavage device, the so-called coil inlet temperature, abbreviated CIT, can range from approx. 600° C. up to and including 650° C lie.

In the outlet area, the temperature of the products to be discharged, in particular the so-called cracked gas, can be in the range from approx. 750° C. up to and including 900° C., in particular in the range from approx. 830 up to and including 870° C. If necessary, the temperature of the products to be discharged, in particular the so-called cracked gas, in the outlet area of the cracking device, in particular in the outlet area of the cracking tube of the cracking device, the possibly so-called coil outlet temperature, abbreviated COT, in the range of approx. 750 °C up to and including

900 °C, in particular in the range from approx. 830 up to and including 870 °C.

If appropriate, it is provided that the temperature of the supplied hydrocarbon, the supplied hydrogen and/or the supplied water is in the range from 600° C. to 650° C. inclusive.

If necessary, it is provided that the temperature of the discharged hydrocarbon, the discharged hydrogen, and/or the discharged water in the outlet area of the cracking device, in particular in the outlet area of the cracking tube; is in the range from 750°C up to and including 900°C, in particular in the range from 830°C up to and including 870°C and is in particular 850°C.

In the context of the present invention, the cracking device, in particular the so-called cracking coil, can be the reactor used in conventional cracking devices, in particular steam crackers, in particular the reactor used

Tubular reactor, in which the actual steam cracking takes place, are understood. Optionally, it is provided that the temperature of the cracking device,

in particular in the exit area of the splitting device, is in the range from 750°C to 900°C inclusive.

If necessary, it is provided that the pressure of the cracking device, in particular in the outlet region of the cracking device, preferably in the so-called cracking tube outlet, in

range is 1.2 bar up to and including 3 bar.

If appropriate, it is provided that the residence time in the cracking device, in particular in the cracking device, preferably in the so-called cracking tube, is less than one second.

In the context of the present invention, residence time can be understood to mean the length of time the feed stream, in particular the components of the feed stream, remain in the splitting device. In other words, the residence time is the time that the feed stream, in particular the components of the

Feed stream required from the slotted tube inlet to the slotted tube outlet.

If necessary, it is provided that the process steam to hydrocarbon ratio, in particular in the cracking device, is in the range from 0.3 kg/kg to

0.8 kg/kg inclusive.

Optionally, the cracker feed stream is envisaged to be naphtha

or ethane.

If necessary, it is provided that the cracking device is operated without a catalyst

is.

Catalysts may be required for hydrogenation and/or hydrocracking. A cracking device, in particular the thermal cracking device, preferably the so-called thermal cracking coil, does not require one for steam cracking

Catalyst.

A reforming device, in particular a so-called steam reforming device, a so-called steam methane reformer (SMR), can have at least one thermal cracking device, which optionally with

filled with a catalyst. A reformer splits, in particular

cracks, optionally hydrocarbons, so-called CHs, and water, so-called H,O, into hydrogen, so-called H, and carbon dioxide, so-called CO.

The methane used, so-called CH4, can be partially reused or recycled in the reforming device, in particular used as a recycle stream. The recycle stream may also contain hydrogen, so-called H − .

In the context of the present invention, the process steam to hydrocarbon ratio can result from the process steam mass in relation to the hydrocarbon mass entering the splitting device, the so-called splitting coil. In this calculation, the hydrogen entering the cracker

may not be taken into account and/or counted.

In particular, the invention relates to a refinery for the production of

Hydrocarbons, wherein the refinery comprises an arrangement according to the invention.

In particular, the invention relates to a refinery for the production of hydrocarbons, the refinery by the arrangement according to the invention

is formed.

In particular, the invention relates to a method for producing hydrocarbons with an arrangement, in which, in particular so-called green,

Hydrogen is produced in a hydrogen production device.

In particular, the invention relates to a method for producing hydrocarbons with an arrangement, in which, in particular so-called green, hydrogen in an electrolyzer for water electrolysis or a reforming device, preferably a steam reforming device or a

Methane pyrolysis device is manufactured.

Optionally, it is provided that a feed stream containing hydrocarbons, and the hydrogen produced a cracking device, in particular one

Steam crackers are fed.

In particular, the emissions per tonne of ethene produced and/or HVC produced in the cracking device can be lower than in the case of a cracking device without the supply of hydrogen as a result of the supply of, in particular so-called green, hydrogen. Within the scope of the present invention, emissions can include carbon dioxide, nitrogen oxides and/or

dust are understood.

Optionally, it is provided that the amount of hydrogen fed to the cracker is adjusted such that emissions per tonne of ethene produced

and/or HVC produced are less than conventional crackers.

Optional regulation and/or control of the cracker, in particular the operating parameters of the cracker and/or the amount of hydrogen fed to the cracker, so that the emissions of the cracker per tonne of ethene produced and/or HVC produced are lower than with conventional cracker and/or cracker , which no hydrogen

is supplied.

Optionally, it is provided that hydrocarbons are produced with the cracking device, the hydrocarbons produced being at least partially

consist of the produced, in particular so-called green, hydrogen. If necessary, it is provided that the hydrogen production device, in particular exclusively, from a renewable energy source, in particular from solar energy,

powered by bioenergy, hydroelectric power and/or wind energy.

Optionally, it is provided that by the hydrogen production device

Hydrogen, in particular so-called green hydrogen, is produced.

If necessary, it is provided that, in particular in a combustion chamber, the cracking device for heating a fuel, in particular a fuel gas, and

oxygen is supplied.

If necessary, it is provided that the oxygen supplied to the cracking device is produced, in particular exclusively, by the hydrogen production device

and in particular the oxygen formed during the electrolysis of water.

If appropriate, it is provided that at least part of the output stream of the cracking device is fed to a reforming device, in particular a steam reforming device or a methane pyrolysis device, of the arrangement

is supplied.

Optionally, it is provided that the output stream of the cracking device, in particular the hydrocarbons contained in the output stream, at least partially from the produced by the hydrogen production device, in particular

the so-called green, hydrogen.

If necessary, it is provided that at least part of the output current

contained methane is fed to a reforming device of the arrangement.

Optionally, it is provided that the methane, at least partially from the produced by the hydrogen production device, in particular the so-called

green, hydrogen consists.

If necessary, it is provided that through the reforming device,

in particular so-called green hydrogen is produced. If necessary, it is provided that by the reforming device from the im

Output stream of the cracker contained hydrocarbons, in particular

Methane, in particular so-called green hydrogen, is produced.

Optionally, it is provided that at least part of the output stream of the cracking device and/or at least part of that produced by the hydrogen production device and/or by the reforming device

Hydrogen are fed to a hydrogenation plant of the arrangement.

If necessary, it is provided that the output stream, in particular the hydrocarbons contained in the output stream, of the cracking device consists in particular at least partially of the, in particular so-called green, hydrogen.

If necessary, it is provided that the hydrogenation plant hydrocarbons

getting produced.

Optionally, it is provided that the hydrogenation plant from the hydrocarbons contained in the output stream of the cracker

hydrocarbons are produced.

If necessary, it is provided that the hydrocarbons produced with the hydrogenation plant are at least partly made up of, in particular so-called green,

hydrogen exist.

If necessary, it is provided that the hydrocarbons produced by the hydrogenation plant consist of more, in particular green, hydrogen than that of the

Hydrocarbons supplied to the hydrogenation plant.

If necessary, it is provided that the, in particular green, molecular hydrogen contained in the output stream of the cracking device and/or the hydrogenation plant is separated, in particular completely, from the hydrocarbons and

fed to the cracker and/or the hydrogenation plant. Optionally, it is provided that an exit of the molecular hydrogen from the

Arrangement, in particular the cracking device, essentially prevented or

is reduced.

If necessary, it is provided that the, in particular so-called green, hydrogen

is separated from the hydrocarbons in a separator.

If necessary, it is provided that the separated molecular, in particular green, hydrogen of the arrangement, in particular the cracking device and / or

Hydrogenation plant, is supplied.

If necessary, it is provided that the amount of molecular hydrogen, which the arrangement, in particular the cracking device, is fed is adjusted such that the amount of hydrogen in the feed stream and the amount of molecular hydrogen fed in, the amount of hydrogen in the output stream

Arrangement, in particular the cracking device corresponds.

If necessary, it is provided that the amount of molecular hydrogen fed to the arrangement, in particular the cracking device, is adjusted in such a way that the amount of hydrogen in the hydrocarbons fed to the cracking device, and the amount of molecular hydrogen fed to the cracking device, corresponds to the amount of hydrogen in the Hydrocarbons in the outlet stream

Arrangement, in particular the cracking device corresponds.

Optionally, it is provided that the amount of molecular hydrogen which is supplied by the hydrogen production device to the cracking device is adjusted in such a way that the amount of hydrogen in the feed stream to the cracking device and the amount of molecular hydrogen supplied corresponds to the amount of hydrogen in the

Output current corresponds to the arrangement.

If necessary, the amount of, in particular molecular, hydrogen, which is supplied to the arrangement, in particular the cracking device, is selected or adjusted and/or the arrangement, in particular the cracking device, is operated in such a way that the amount of, in particular molecular, hydrogen of those corresponds to the arrangement, in particular from the cracking device, the

Separation device and / or the steam reforming device is discharged.

This mode of operation may be advantageous if, for example, the hydrogen production device and/or another hydrogen producer is not available and/or if the hydrogen balance of the refinery is not known

wants to influence.

If necessary, the amount of hydrogen, in particular molecular, which is supplied to the arrangement, in particular the cracking device, is selected or adjusted and/or the arrangement, in particular the cracking device, is operated in such a way that the amount of hydrogen removed from the arrangement, in particular the cracking device

Amount of, in particular molecular, hydrogen is essentially zero.

In this case, the supplied so-called green hydrogen can optionally be contained in the hydrocarbons discharged and/or in the

Hydrocarbons are incorporated.

This means that the amount of, in particular molecular, hydrogen removed from the arrangement may be equal to, greater than or less than that of the

supplied amount of hydrogen or zero.

If the amount of, in particular molecular, hydrogen removed is zero, the so-called green hydrogen supplied may be in the removed hydrogen

contain hydrocarbons.

If the amount of hydrogen removed is equal to the amount of, in particular molecular, hydrogen fed in, the process may be hydrogen-neutral. That means, where appropriate, that the arrangement, the cracking device and/or the process, the rest of the refinery with respect to the

Hydrogen balance not affected. If the removed amount of, especially molecular, hydrogen is greater or

is equal to the supplied amount of, in particular molecular, hydrogen needs

you may no longer have a hydrogen source. If the hydrogen source

possibly temporarily not available, you can still use hydrogen

commit to use.

Furthermore, the addition of hydrogen can increase the formation of methane in the cracker. From methane with the reforming device, in particular with the methane pyrolysis, in particular so-called green, hydrogen

getting produced.

If necessary, the supplied amount of, in particular molecular, hydrogen is selected or adjusted and/or the arrangement, in particular the cracking device, is operated in such a way that essentially no methane leaves the arrangement, in particular the cracking device. This means that, if necessary, the methane produced in the arrangement and/or supplied from outside can be converted in the arrangement. In particular, the methane can be used to produce hydrogen and/or as heating gas.

If necessary, the supplied quantity of, in particular molecular, hydrogen is selected or adjusted and/or the arrangement, in particular the cracking device, is operated in such a way that no methane is introduced into the arrangement, in particular the cracking device, in particular from outside. This may mean that the methane that is produced and required in the arrangement can be generated and/or converted in the arrangement. In particular, the methane

used for hydrogen production and/or as heating gas.

If necessary, it is provided that the arrangement of the method according to the invention

is trained.

Optionally, it is provided that the method according to the invention for the production

of hydrocarbons is carried out on an arrangement according to the invention.

If necessary, it is provided that the method steps of the method are as before

described follow each other.

If necessary, it is provided that the specified semantic order of the

Process steps are not in chronological order.

With the arrangement according to the invention and/or with the method according to the invention, the sustainability of the cracking device, in particular of the steam cracker, can be increased since, among other things, the required amount of energy in the

cracker sinks.

This may be due to the fact that the addition of hydrogen may reduce the required enthalpy difference between a point at the entrance to the cracking device, in particular the so-called cracking tube inlet, and a point at the outlet of the cracking device, in particular the so-called cracking tube outlet. As a result, less heating gas may be needed and less

emissions occur.

The reduction in the required amount of energy or emissions in the cracking device can be further increased by adding oxygen to the air supplied for combustion, since the addition of oxygen

if necessary, the air mass flow to be heated can be reduced.

The heating power required can optionally be between a point at the entrance to the cracking device, in particular the so-called cracking tube inlet, and a point at the outlet of the cracking device, in particular the so-called cracking tube outlet.

additionally by the introduction of heat generated by means of electricity, in particular

electrical heating power, can be reduced.

With the arrangement according to the invention and/or with the method according to the invention, the sustainability of the cracking device, in particular of the steam cracker, can be increased because, among other things, the required heat flow density

is reduced by the tube wall of the splitter of the cracker.

In the arrangement according to the invention and / or with the invention

Process can the sustainability of the cracker, in particular of the

Steamcracker, are increased, among other things, the surface temperature of the

Splitting device of the cracking device is reduced.

In other words, it may be possible to thermally relieve the cracker and / or to increase the firing efficiency, although the

Feed stream, in particular through the addition of hydrogen, is increased.

This may make it possible to increase the service life and/or the availability of the cracking device and in particular the cleavage device with the same yield, in particular the yield and/or production quantity of ethene, in that the furnace running time per decoking cycle can be extended in particular. In other words, the service life of the cracking device can optionally be increased by the design of the arrangement according to the invention and/or by the method according to the invention. In particular, it can be provided that the points in time when decoking of the cracking device is necessary are further in time

lie apart.

In the context of the present invention, the products, ie in particular the mass fractions of the hydrocarbons, so-called CHs, and / or the hydrocarbon mixtures, so-called CH mixtures, based on the yield

input current can be understood.

In other words, in the arrangement according to the invention or by using the method according to the invention, the fire-related emissions, in particular the CO emissions, can be reduced, the energy consumption per ton of high-value chemicals (HVC) and the production of green HVCs in the

Cracking device, especially in the steam cracker, are increased.

Within the scope of the present invention, HVCs can include, in particular, ethylene,

Propylene, 1,3-butadiene, benzene, toluene and/or mixed xylenes are understood.

The arrangement according to the invention can be both existing and future

Cracking devices, particularly steam crackers, include.

The inventive method can both existing and future

Cracking devices, in particular steam crackers, are applied.

If necessary, it is provided that, in particular molecular and/or so-called green hydrogen, is fed to the cracking device, in particular to the steam cracker

becomes.

The arrangement according to the invention and/or the method according to the invention may make it possible to reduce the carbon dioxide emissions, in particular the so-called CO »footprint, per tonne of ethene in the output stream

reduce cracking device.

The arrangement according to the invention and/or the method according to the invention may make it possible to reduce the carbon dioxide emissions, in particular the so-called CO footprint, per tonne of high-value chemicals in the output stream of the cracking device.

With the arrangement according to the invention and/or with the method according to the invention, in particular through the supply of, in particular, molecular and so-called green hydrogen, it is possibly possible to use the cracking device, in particular the steam cracker, to produce hydrocarbons which are at least partially composed of the in particular green, hydrogen exist or

are formed at least partially from the green hydrogen in particular.

With the arrangement according to the invention and/or with the method according to the invention, it may be possible to increase the profitability of the cracking device,

especially the steam cracker.

The arrangement according to the invention and / or with the method according to the invention, in particular by the supply of, in particular molecular and so-called green, hydrogen, it is optionally possible to increase the proportion of

Increase methane and/or ethene in the cracker exit stream.

With the arrangement according to the invention and/or with the method according to the invention, in particular through the supply of, in particular molecular and so-called green, hydrogen, it is optionally possible to reduce the proportion of 1,3-butadiene, benzene and/or the residue, in particular heating oil and/or so-called pyrolysis gasoline residue, in the output stream of the cracker and

optionally at the same time to increase the production volume of ethene.

With the arrangement according to the invention and/or with the method according to the invention, in particular through the supply of, in particular molecular and so-called green, hydrogen, it may be possible to increase the yield in

Set the output current of the cracker.

The inventor states that according to the Gibbs energy or the Gibbs phase rule, there is only a very small number of possible combinations of products per use in a conventional cracking device. In conventional cracking devices, non-significant side reactions such as coking and the like are usually neglected for the sake of simplicity, which means that there are usually only two degrees of freedom per feed composition and/or two controlled variables. Therefore, in conventional crackers, all possible product mixtures of a feed composition may reside on one "surface". The arrangement according to the invention and/or with the method according to the invention, in particular the addition or supply of hydrogen to the cracking device according to the invention, makes it possible to change the composition of the feedstock, which may result in a further degree of freedom and/or a further controlled variable compared to conventional cracking devices. The product mixtures that can be produced by the arrangement according to the invention and/or with the method according to the invention are therefore no longer limited to this “area”. Compared to the conventional mode of operation of cracking devices, in particular of steam crackers, product yields that were previously impossible can be achieved. As a result, the product yield and/or the contribution margin of the cracking device can be better optimized by the arrangement according to the invention and/or with the method according to the invention

be increased.

With the arrangement according to the invention and/or with the method according to the invention, in particular through the supply of, in particular molecular and so-called green, hydrogen, it may be possible to prevent coking in the cracking device and/or the formation of so-called heavy “products” in the

to reduce cracking device.

In the context of the present invention, “heavy products” can be understood as meaning hydrocarbons with more than five carbon atoms, in particular benzene, toluene, pyrolysis gasoline and/or so-called pyrolysis gasoline residue

become.

With the arrangement according to the invention and/or with the method according to the invention, in particular through the supply of, in particular molecular and so-called green, hydrogen, it may be possible to circumvent the various conventional limitations of the cracking device, in particular a steam cracker. The limitation can possibly be caused by the tube wall temperature, the coking rates, in particular the coking rate in the cracking tube and/or the coking rate in the quench cooler, the pressures and/or the firing capacity. This can optionally compared to conventional cracking devices higher amounts of products, in particular

higher amounts of ethene are produced.

With the arrangement according to the invention and/or the method according to the invention, cheaper feeds can optionally be used as the feed stream for the cracking device due to the increase in or the same ethene production with a simultaneous extension of the furnace running time. In the context of the present invention, cheaper feeds can be understood as meaning feed streams which can be converted to fewer HVCs in a conventional cracker compared to expensive feeds

are.

By adding hydrogen to the use of the cracking device according to the invention,

in particular the cleavage device, optionally the cracking device,

in particular the splitting device, thermally relieved and the production capacity of

Cracking device to be increased.

With the arrangement according to the invention and/or the method according to the invention, what is known as load balancing can optionally be carried out between the hydrogen production device and the cracking device. In other words, if necessary, the cracker on the

Hydrogen manufacturing device to be debottlenecked.

With the arrangement according to the invention and/or the method according to the invention, the ethene production can be increased by the addition of hydrogen, if appropriate with the same amount of hydrocarbon used, without

possibly to reduce the propene production.

Since a metathesis plant may produce propene from ethene, it is therefore advantageous to increase ethene production by adding hydrogen, since other known methods for increasing ethene production, in particular raising the temperature at the cracking tube outlet, known as COT raising, Ethen though

increase, but lower propene, which is comparatively counterproductive.

With the arrangement according to the invention and/or the method according to the invention, if ethane and hydrogen are fed in in the feed stream, the production of ethene can be increased if the unreacted ethane is fed back to the cracking device, ie in particular in what is known as total recycling

to be led. If necessary, it is provided that the arrangement has at least one feed arrangement, in particular one, two, three, four, five, six, seven, eight, nine,

ten or more feed assemblies.

Optionally, it is provided that the or a further feed arrangement

Cracking device feeds the feed stream.

If necessary, it is provided that the or a further supply arrangement of the cracking device supplies the fuel, in particular the heating gas, the oxygen and/or the air.

If necessary, it is provided that the or a further feed arrangement of the cracking device, in particular the steam cracker, preferably the splitting device,

Hydrocarbons, hydrogen and / or water feeds.

If necessary, it is provided that the or a further feed arrangement of the cracking device separates the from the at least one separating device

supplies molecular hydrogen.

If necessary, it is provided that the or a further feed arrangement of the hydrogenation plant separates the from the at least one separating device

supplies molecular hydrogen.

If necessary, it is provided that the or another feed arrangement of the reforming device, in particular the steam reforming device or the methane pyrolysis device, feeds at least part of the output stream of the cracking device, in particular that in the output stream of the cracking device

contained methane feeds.

Optionally, it is provided that the or a further feed arrangement of the reforming device, in particular the steam reforming device or the

Methane pyrolysis device feeding methane from an external source.

Optionally, it is provided that the or a further supply assembly produced by the reforming device molecular hydrogen

Cracking device and / or the hydrogenation plant supplied. Optionally, it is provided that the or a further feed arrangement

Hydrogenation plant at least part of the output stream of the cracker

supplies.

If necessary, it is provided that the or a further supply arrangement of the hydrogenation plant supplies at least a part of the, in particular so-called, produced by the hydrogen production device and/or by the reforming device

green, supplies hydrogen.

If appropriate, it is provided that the or a further feed arrangement of the metathesis plant feeds at least part of the output stream of the cracking device

supplies.

Optionally, it is provided that the or a further feed arrangement, the products of the arrangement, in particular the products of the cracker, the products of the hydrogenation plant and / or the products of the metathesis plant from the

dissipates arrangement.

Other features of the invention may arise from the

Claims, the description of the exemplary embodiments and the figure.

The invention will now be exemplified, not exclusively and/or

non-limiting embodiments explained further.

Fig. 1 shows a schematic diagram of a first embodiment of the

arrangement according to the invention.

Unless otherwise indicated, reference numerals correspond to the following

Components: Cracking Device 1, Feed Assembly 2, Hydrogen Production Device 3, Renewable Energy Source 4, Feed Stream 5, Steam 6, Hydrogen 7, Oxygen 8, Air 9, Separation Device 10, Output Stream 11, Steam Reforming Device 12,

fuel oil 13, methane 14, hydrogenation plant 15, product 16 and metathesis plant 17. Figure 1 shows a schematic diagram of the present invention

Arrangement, which set up for the production of hydrocarbons and / or

is trained.

The arrangement includes a cracking device 1, namely a steam cracker, and a

feeding arrangement 2.

The feed assembly 2 leads the cracker 1 a feed stream 5, which

Contains hydrocarbons, and steam 6 too.

The cracking device 1 is set up for steam cracking of the hydrocarbons

and/or trained.

The arrangement also includes a hydrogen production device 3. According to this embodiment, the hydrogen production device 3 is designed as an electrolyzer for the electrolysis of water. Alternatively, the hydrogen production device 3 can also be designed as a reforming device, preferably as a steam reforming device 12 or a methane pyrolysis device.

The hydrogen production device 3 is for the production of, in particular

so-called green, hydrogen 7 set up and / or trained.

The feed arrangement 2 feeds at least part of the hydrogen 7 produced by the hydrogen production device 3 , in particular so-called green hydrogen 7 , to the cracking device 1 . In an embodiment that is not shown, the cracking device 1 can also be fed with conventional hydrogen 7 in addition to the so-called green hydrogen

become.

According to this embodiment, the feed arrangement 2 of the cracking device 1 supplies molecular, in particular so-called green, hydrogen 7 in the range from 0.05 wt.% Up to and including 5 wt.% Based on the feed stream 5 of the cracking device 1,

in particular to the hydrocarbons in feed stream 5.

The cracker 1 produces hydrocarbons, the produced

Hydrocarbons at least partially from the of the

Hydrogen production device 3 manufactured, in particular the so-called green,

hydrogen 7 exist.

According to this embodiment, the reactions that also take place in conventional cracking devices 1 essentially take place in the cracking device 1 . This makes it possible to mix the supplied hydrogen 7 with that of the cracking device 1

to chemically combine supplied hydrocarbons.

According to this embodiment, the arrangement comprises a renewable energy source 4, namely a solar energy utilization device. Alternatively, the arrangement can also be a bioenergy utilization device, a hydroelectric power utilization device and/or a wind energy utilization device,

include.

The hydrogen production device 3 is powered by the renewable energy source 4, namely solar energy. As a result, the hydrogen production device 3

according to this embodiment, in particular so-called green, hydrogen 7 ago.

The reactions that also take place in conventional hydrogen production devices 3 essentially take place in the hydrogen production device 3 . This makes it possible to split water into hydrogen 7 and oxygen 8 with the help of electricity. Since the electric current comes from a renewable energy source 4, it is possible with the hydrogen production device 3

so-called green hydrogen 7 to produce.

According to this embodiment, the feed assembly 2 leads to a combustion chamber

Cracking device 1 a fuel, in particular a heating gas.

According to this embodiment, the feeding arrangement 2 leads to the combustion of the

Heating gas to the combustion chamber of the cracking device 1, oxygen 8 and/or air 9.

The oxygen 8 supplied to the combustion chamber is, in particular exclusively, produced by the hydrogen production device 3, in particular in the electrolysis of

water resulting oxygen 8.

According to this embodiment, the oxygen produced by the hydrogen production device 3 in the electrolysis of water 8 before entering the cracking device 1 with the fuel gas, in particular methane 14, and / or

supplied air 9 mixed.

According to this embodiment, the arrangement comprises a separation device 10. The separation device 10 separates the molecular, in particular green, hydrogen 7, in particular, contained in the output stream 11 of the cracking device 1

completely, from the hydrocarbons contained in the output stream 11.

The feed arrangement 2 feeds the molecular, in particular green, hydrogen 7 separated by the separating device 10, in particular completely, to the cracking device 1 as a so-called recycle stream, so that an escape of the molecular hydrogen / from the arrangement is essentially prevented

or is reduced.

In other words, in the separating device 10, the molecular, in particular green, hydrogen 7 contained in the output stream 11 of the cracking device 1 is, in particular, completely separated from the hydrocarbons. This hydrogen 7 is then returned to the cracking device 1 . According to this embodiment, this essentially prevents or prevents the molecular hydrogen 7 from escaping from the arrangement, in particular from the cracking device 1

reduced. Optionally, the feed assembly 2 can also at least a part of the

Cracking device 1 products generated, in particular hydrogen /, methane and / or

Fuel oil 13, in particular from the separation device 10, discharge from the arrangement.

According to this embodiment, the arrangement comprises a reforming device, namely a steam reforming device 12. Alternatively, the reforming device can also be designed as a methane pyrolysis device

be.

The feed arrangement 2 carries at least part of the output stream 11 of the cracking device 1, in particular at least part of the output stream 11

contained methane 14, the reforming device.

The output stream 11 of the cracking device 1, in particular the methane 14 contained in the output stream 11 of the cracking device 1, consists at least partially of the produced by the hydrogen production device 3, in particular the so-called

greens, hydrogen 7.

The reforming device is set up to produce hydrogen/from methane 14 , so that the reforming device produces hydrogen 7 , in particular so-called green hydrogen.

In other words, at least part of the output stream 11 of the cracking device 1, in particular at least part of the methane 14 contained in the output stream 11, is fed to the reforming device of the arrangement. The output stream 11 of the cracking device 1, in particular the methane 14, consists at least partially of the so-called green hydrogen / produced by the hydrogen production device 3. This will in the

Reforming device, in particular so-called green, hydrogen 7 produced.

According to this embodiment, the arrangement comprises a hydrogenation plant 15.

The feed assembly 2 performs at least part of the output stream 11 of

Cracking device 1, which contains in particular hydrocarbons, the

Hydrogenation plant 15 to.

The output stream 11 of the cracking device 1 comprises hydrocarbons which are produced at least partially from the hydrogen production device 3,

in particular the so-called green, hydrogen 7 exist.

The feed arrangement 2 feeds at least part of the hydrogen 7 generated by the reforming device to the hydrogenation plant 15 . Alternatively, the supply arrangement 2 can also supply part of the hydrogen produced by the hydrogen production device 3 / to the hydrogenation system 15 . If necessary, the supply arrangement 2 can also supply at least part of the hydrogen 7 produced by the reforming device as a product of the arrangement

take away

The hydrogenation plant 15 is set up for the hydrogenation of hydrocarbons.

The hydrogenation plant 15 produces hydrocarbons, the hydrocarbons produced being at least partially made up of the, in particular the so-called green,

hydrogen 7 exist.

Furthermore, the hydrocarbons produced by the hydrogenation plant 15 consist of more, in particular green, hydrogen 7 than that of the hydrogenation plant 15

supplied hydrocarbons.

The separating device 10 separates the molecular, in particular green, hydrogen 7 contained in the output stream 11 of the hydrogenation plant 15, in particular completely, from that contained in the output stream 11 of the hydrogenation plant

hydrocarbons.

The feed arrangement 2 feeds the molecular, in particular green, hydrogen 7 separated by the separating device 10, in particular completely, to the hydrogenation plant 15 as a so-called recycle stream, so that the molecular hydrogen 7 may escape from the arrangement, in particular the

Hydrogenation plant 15 is essentially prevented or reduced.

In other words, in the separation device 10, the molecular, in particular green, hydrogen 7 contained in the output stream 11 of the hydrogenation plant 15 is separated, in particular completely, from the hydrocarbons. This hydrogen 7 is then returned to the hydrogenation plant 15 . According to this embodiment, this essentially prevents or prevents the molecular hydrogen 7 from escaping from the arrangement, in particular from the hydrogenation plant 15

reduced.

The hydrocarbons produced by the hydrogenation plant 15 and/or cracking device 1 can be discharged from the feed arrangement 2 as product 16

become.

In other words, at least part of the output stream 11 of the cracking device 1 and at least part of the hydrogen 7 produced by the hydrogen production device 3 and/or by the reforming device is fed to the hydrogenation plant 15 of the arrangement. The output stream 11 of the cracking device 1 consists at least partially of the, in particular so-called green, hydrogen 7. The hydrogenation plant 15 thus produces hydrocarbons which at least partially consist of, in particular, so-called green hydrogen /. According to this embodiment, the hydrocarbons produced by the hydrogenation plant 15 consist of more, in particular green, hydrogen 7 than that of the hydrogenation plant 15

supplied hydrocarbons.

According to this embodiment, the arrangement comprises a metathesis system 17.

The feed assembly 2 performs at least part of the output stream 11 of

Cracking device 1, which contains in particular hydrocarbons, the metathesis

Attachment 17 to.

The output stream 11 of the cracking device 1 consists at least partly of that produced by the hydrogen production device 3, in particular the so-called

greens, hydrogen 7.

Metathesis plant 17 is designed to convert four-carbon hydrocarbons and ethene to three-carbon hydrocarbons, specifically n-butene and ethene to propene,

furnished.

The metathesis plant 17 produces hydrocarbons with three carbon atoms, in particular propene, with the hydrocarbons produced with three carbon atoms being at least partially made up of the, in particular the so-called green, produced by the hydrogen production device 3

hydrogen 7 exist.

The hydrocarbons produced by the metathesis plant 17 can be used as a product

16 are discharged from the feed arrangement 2.

If necessary, the products 16, in particular C,He, Cz3Hs and/or so-called hydrogenated C4s, can be fed at least partially to the cracking device 1.

According to this embodiment, the cracking device 1 comprises at least one

Splitting device, a so-called splitting coil.

The feed arrangement 2 feeds the cracking device hydrocarbons, hydrogen 7

and/or water too. The temperature of the supplied hydrogen 7, the feed stream 5 and / or the

According to this embodiment, the water supplied is in the range from 600° C. to 650° C. inclusive.

According to this embodiment, the temperature of the cracking device 1, in particular in the outlet region of the cracking device, is in the range from 750° C. to 900° C. inclusive.

According to this embodiment, the pressure of the cracking device 1, in particular in the outlet region of the cracking device, is in the range from 1.2 bar to

including 3 bars.

According to this embodiment, the process steam to hydrocarbon ratio, in particular in the cracking device 1, is in the range of 0.3 kg/kg up to and including 0.8 kg/kg.

The feed stream 5 of the cracker 1 according to this embodiment comprises naphtha or ethane.

The cracking device 1 according to this embodiment becomes essentially

operated without a catalyst.

According to this embodiment, the arrangement is part of a refinery.

The feed arrangement 2 leads the products 16, in particular hydrogen /, methane 14 and / or fuel oil 13, from. If necessary, the hydrogen 7 is fed back to the cracking device 1 . Optionally, the methane 14 of the cracking device 1 as

supplied heating gas.

In this arrangement, a process for the production of hydrocarbons

performed, which includes the following steps:

Making so-called green, hydrogen 7 in one

Hydrogen production device 3.

Feeding a feed stream 5 containing hydrocarbons and the hydrogen 7 produced by the hydrogen production device 3 to a cracker

1, namely to a steam cracker.

Production of hydrocarbons with the cracking device 1, wherein the hydrocarbons produced at least partially from the produced, in particular

so-called green, hydrogen / consist.

The amount of molecular hydrogen 7 which is fed to the arrangement, in particular the cracking device 1, according to this embodiment is adjusted in such a way that the amount of hydrogen in the feed stream 5 and the amount of molecular hydrogen fed in /, the amount of hydrogen 7 in the output stream 11 der

Arrangement, in particular the cracking device 1 corresponds.

Alternatively, the amount of molecular hydrogen / which is fed to the arrangement, in particular the cracking device 1, can be adjusted such that the amount of hydrogen in the hydrocarbons fed to the cracking device 1 and the amount of molecular hydrogen 7 fed to the cracking device 1 correspond to the amount of hydrogen 7/ the hydrocarbons in the output stream 11 of the arrangement,

in particular the cracking device 1.

If necessary, it is provided that the feed arrangement 2 at least partially feeds the output stream 11 back, in particular the various products 16, to the cracking device, if in particular the steam reforming device 12, hydrogenation plant 15 and/or metathesis plant

17 not working and/or missing.

In all of the embodiments, the feed arrangement 2 can comprise shut-off devices and/or valve devices in order to shut off the feed stream, the output stream and/or the further mass flows in the arrangement of the cracking device 1, the hydrogen production device 3, the separation device 10, the steam reforming device 12, the hydrogenation plant 15 and/or or the metathesis

Attachment 17 to supply and / or to forward.

This configuration can be provided in all embodiments.

With this exemplary configuration, the effects of the present invention can be obtained

become. The invention is not limited to the illustrated embodiments, but

includes any arrangement, refinery and process according to the following

patent claims.

44 / 62

Claims (1)

patent claims 1... Arrangement for the production of hydrocarbons comprising a cracking device (1), in particular a steam cracker, and a feed arrangement (2), the feed arrangement (2) of the cracking device (1) containing a feed stream (5) containing hydrocarbons and steam (6) and wherein the cracking device (1) is set up for steam cracking the hydrocarbons, in particular for converting long-chain hydrocarbons with steam (6) to short-chain hydrocarbons, characterized, - that the arrangement comprises a hydrogen production device (3), in particular an electrolyser for water electrolysis and/or a reforming device, preferably a steam reforming device (12) or a methane pyrolysis device, - that the hydrogen production device (3) is set up for the production of, in particular so-called green, hydrogen (7), - that the supply arrangement (2) supplies at least part of the hydrogen (7) produced by the hydrogen production device (3), in particular so-called green hydrogen (7), to the cracking device (1), - that the cracking device (1) produces hydrocarbons, - And that the hydrocarbons produced at least partially from the hydrogen production device (3) produced, in particular the so-called green, hydrogen (7) exist. 2. Arrangement according to claim 1, characterized in that - that the arrangement, in particular the hydrogen production device (3), draws electricity from a renewable energy source (4), in particular from solar energy, bioenergy, hydropower and/or wind energy, - And / or that the arrangement a renewable energy source (4), in particular a solar energy utilization device, a bioenergy utilization device, a hydropower utilization device and/or a wind energy utilization device, includes, wherein the hydrogen production device (3) is operated by the renewable energy source (4), - and / or that the hydrogen production device (3), in particular so-called greens, produces hydrogen (7). 3. Arrangement according to claim 1 or 2, characterized in that - that the feed arrangement (2), in particular a combustion chamber, supplies a fuel, in particular a fuel gas, to the cracking device (1), - that the supply arrangement (2) supplies oxygen (8) and/or air (9) to the combustion chamber, in particular the combustion chamber, of the cracking device (1), - that optionally the oxygen (8) supplied to the combustion chamber is produced, in particular exclusively, by the hydrogen production device (3), in particular the oxygen (8) produced during the electrolysis of water, - that the oxygen (8) produced by the hydrogen production device (3), in particular the oxygen produced during the electrolysis of water, is mixed with the fuel and/or the air (9) that may be supplied, in particular before it enters the cracking device (1). , - that the arrangement optionally includes a separating device (10), - that optionally the separating device (10) separates the molecular, in particular green, hydrogen (7) contained in the output stream (11) of the cracking device (1), in particular completely, from the hydrocarbons contained in the output stream (11), - and that, if necessary, the feed arrangement (2) feeds the molecular, in particular green, hydrogen (7) separated by the separating device (10), in particular completely, to the cracking device (1), so that the molecular hydrogen (7) may escape from the arrangement , In particular the cracking device (1), essentially prevented or is reduced. 4. Arrangement according to one of the preceding claims, characterized in that that the arrangement comprises a reforming device, preferably a steam reforming device (12) or a methane pyrolysis device, and/or that the feed arrangement (2) feeds at least part of the output stream (11) from the cracking device (1), in particular at least part of the methane (14) contained in the output stream (11), to the reforming device, and/or that the output stream (11) of the cracking device (1), in particular the methane (14) contained in the output stream (11) of the cracking device (1), consists at least partially of the methane (14) produced by the hydrogen production device (3), in particular the so-called green hydrogen (7) and/or that the reforming device is set up to produce hydrogen (7) from methane (14), and / or that the reforming device, in particular so-called greens, produces hydrogen (7). Arrangement according to one of the preceding claims, characterized in that the arrangement comprises a hydrogenation plant (15) and/or that the feed arrangement (2) contains at least part of the output stream (11) of the cracking device (1), which contains in particular hydrocarbons, of the hydrogenation plant (15) and/or that the output stream (11) of the cracking device (1) contains hydrocarbons, which optionally consist at least partially of the hydrogen (7) produced by the hydrogen production device (3), in particular the so-called green hydrogen, and/or that the supply arrangement (2) supplies at least part of the hydrogen (7) produced by the hydrogen production device (3) and/or by the reforming device to the hydrogenation plant (15), and/or that the hydrogenation plant (15) is set up for the hydrogenation of hydrocarbons, and/or that the hydrogenation plant (15) produces hydrocarbons, wherein the hydrocarbons produced at least partially from the hydrogen production device (3), in particular the so-called green hydrogen (7), and/or that the hydrocarbons produced by the hydrogenation plant (15) consist of more, in particular green, hydrogen (7) than the hydrocarbons fed to the hydrogenation plant (15), and/or that the arrangement optionally comprises a separating device (10), that, if necessary, the separating device (10) separates the molecular, in particular green, hydrogen (7) contained in the output stream (11) of the hydrogenation plant (15), in particular completely, from the hydrocarbons contained in the output stream (11), and that the feed arrangement (2) supplies the molecular, in particular green, hydrogen (7) separated by the separating device (10), in particular completely, to the cracking device (1) and/or the hydrogenation plant (15), so that the molecular hydrogen can optionally escape Hydrogen (7) from the arrangement, in particular the Hydrogenation plant (15), is essentially prevented or reduced. Arrangement according to one of the preceding claims, characterized in that the arrangement comprises a metathesis plant (17) and/or that the feed arrangement (2) contains at least part of the output stream (11) of the cracking device (1), which contains in particular hydrocarbons, to the metathesis plant (17), and/or that the output stream (11) of the cracking device (1) optionally consists at least partially of the hydrogen (7) produced by the hydrogen production device (3), in particular the so-called green hydrogen, and/or that the metathesis plant (17) is set up to convert hydrocarbons with four carbon atoms and ethene into hydrocarbons with three carbon atoms, in particular n-butene and ethene into propene, and/or that the metathesis plant (17) optionally converts hydrocarbons with three carbon atoms , In particular propene, manufactures, wherein the produced hydrocarbons having at least three carbon atoms partly from that produced by the hydrogen production device (3), in particular the so-called green hydrogen (7). 7. Arrangement according to one of the preceding claims, characterized in that the feed arrangement (2) of the cracking device (1) molecular, in particular so-called green, hydrogen (7) in the range of 0.05 wt.% Up to and including 5 wt.%, In particular 0.5 wt.% Up to and including 1.5 wt.%, Based on the feed stream (5) of the cracking device (1), in particular on the hydrocarbons in the feed stream (5), preferably on the so-called dry application stream (5) feeds. 8. Arrangement according to one of the preceding claims, characterized in that - that the cracking device (1) comprises at least one splitting device, a so-called splitting coil, - and/or that the feed arrangement (2) feeds hydrocarbons, hydrogen (7) and/or water to the splitting device, - and/or that the temperature of the supplied hydrocarbon, the supplied hydrogen (7) and/or the supplied water is in the range from 600°C to 650°C inclusive. 9. Arrangement according to one of the preceding claims, characterized in that - that the temperature of the cracking device (1), in particular in the outlet area of the cracking device, is in the range from 750°C up to and including 900°C, in particular in the range from 830°C up to and including 870°C and is in particular 850°C, - and/or that the pressure of the cracking device (1), in particular in the outlet area of the cracking device, is in the range of 1.2 bar up to and including 3 bar, - and/or that the residence time in the cracking device (1), in particular in the cleavage device, is less than one second. - and/or that the process steam to hydrocarbon ratio, in particular in the cracking device (1), is in the range of 0.3 kg/kg up to and including 0.8 kg/kg, - and/or that the feed stream (5) of the cracking device (1) comprises naphtha or ethane, - and/or that the cracking device (1) is substantially catalyst-free is operated. 10. Refinery for the production of hydrocarbons, characterized in that - that the refinery comprises an arrangement according to any one of claims 1 to 9, - or that the refinery by the arrangement according to any one of claims 1 to 9 is formed. 11. A method for producing hydrocarbons with an arrangement, comprising the following steps: - Production of, in particular so-called green, hydrogen (7) in a hydrogen production device (3), in particular an electrolyzer for water electrolysis or a reforming device, in particular a steam reforming device (12) or a methane pyrolysis device, - Feeding a feed stream (5), which contains hydrocarbons, and the produced hydrogen (7) to a cracking device (1), in particular to a steam cracker, - Production of hydrocarbons with the cracking device (1), wherein the hydrocarbons produced are at least partially from the produced, in particular so-called green, hydrogen (7) exist. 12. The method according to claim 11, characterized in that - that the hydrogen production device (3) is operated by a renewable energy source (4), in particular solar energy, bioenergy, hydropower and/or wind energy, so that hydrogen (7), in particular so-called green hydrogen ( 7), is manufactured, - and that optionally, in particular a combustion chamber, the cracking device (1) for heating a fuel, in particular a fuel gas, and oxygen (8) be fed - Wherein the supplied oxygen (8) is produced, in particular exclusively, by the hydrogen production device (3) and in particular at the Electrolysis of water resulting oxygen (8) is. 13. The method according to claim 11 or 12, characterized in that - that at least part of the output stream (11) of the cracking device (1), in particular at least part of the methane (14) contained in the output stream (11), is fed to the reforming device of the arrangement, the output stream (11) of the cracking device (1) , in particular the methane (14), consists at least partially of the hydrogen (7) produced by the hydrogen production device (3), in particular the so-called green hydrogen, and wherein the reforming device produces hydrogen (7), in particular so-called green hydrogen, - and/or that at least part of the output stream (11) of the cracking device (1) and at least part of the hydrogen (7) produced by the hydrogen production device (3) and/or by the reforming device is fed to a hydrogenation plant (15) of the arrangement, wherein the output stream (11) of the cracking device (1) consists in particular at least partially of the, in particular so-called green, hydrogen (7), wherein the hydrogenation plant (15) produces hydrocarbons and the hydrocarbons produced consist at least partially of, in particular so-called green , Hydrogen (7), wherein the hydrocarbons produced by the hydrogenation plant (15) consist of more, in particular green, hydrogen (7) than the hydrocarbons fed to the hydrogenation plant (15), - and/or that the molecular, in particular green, molecular hydrogen (7) contained in the output stream (11) of the cracking device (1) and/or the hydrogenation plant (15) is separated, in particular completely, from the hydrocarbons and sent to the cracking device (1) and / or the hydrogenation plant (15) is fed, so that the molecular hydrogen (7) is essentially prevented from escaping from the arrangement, in particular the cracking device (1). or is reduced. 14. The method according to any one of claims 11 to 13, characterized in that - That the amount of molecular hydrogen (7), which the arrangement, in particular the cracking device (1), is supplied, is adjusted such that the amount of hydrogen in the feed stream (5) and the supplied amount of molecular hydrogen (7) of the amount of Hydrogen (7) in the output stream (11) of the arrangement, in particular the cracking device (1), corresponds to - and/or that the quantity of molecular hydrogen (7), which is fed to the arrangement, in particular to the cracking device (1), is adjusted in such a way that the quantity of hydrogen in the hydrocarbons fed to the cracking device (1) and that to the cracking device (1 ) Supplied amount of molecular hydrogen (7) the amount of hydrogen (7) of the hydrocarbons in the output stream (11) of the arrangement, in particular Cracking device (1), corresponds. 15. The method according to any one of claims 11 to 14, characterized in that the arrangement is designed according to one of claims 1 to 9.